TWI434822B - A manufacture method of methanol and its device thereof - Google Patents

A manufacture method of methanol and its device thereof Download PDF

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TWI434822B
TWI434822B TW100127416A TW100127416A TWI434822B TW I434822 B TWI434822 B TW I434822B TW 100127416 A TW100127416 A TW 100127416A TW 100127416 A TW100127416 A TW 100127416A TW I434822 B TWI434822 B TW I434822B
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methanol
temperature
pressure
carbon dioxide
critical
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TW201307269A (en
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Chang Hsien Tai
Jr Ming Miao
Wu Jang Huang
Yao Nan Wang
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Univ Nat Pingtung Sci & Tech
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    • C25ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
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    • C25B1/00Electrolytic production of inorganic compounds or non-metals
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    • CCHEMISTRY; METALLURGY
    • C25ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25BELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
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    • Y02E60/00Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
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Description

甲醇製作方法及其裝置 Methanol production method and device thereof

本發明係關於一種生質能源的甲醇製作方法,特別是一種提升製作效率且節省製程耗能的甲醇製作方法。 The invention relates to a method for preparing methanol of biomass energy, in particular to a method for preparing methanol which improves production efficiency and saves process energy.

傳統用以生產甲醇燃料的方法,係多採用化學重組的模式,透過觸媒催化甲烷進而轉變為甲醇燃料,惟經由化學重組方式的反應效率較為緩慢,以致於傳統製程方法始終無法達到符合經濟效益需求之目的。 The traditional method for producing methanol fuel is to adopt a chemical recombination mode, which is converted into methanol fuel by catalyst-catalyzed methane, but the reaction efficiency through chemical recombination is slow, so that the traditional process method can not achieve economic benefits. The purpose of the demand.

隨著生質能轉換技術的不斷提升,生質能的轉換利用已普遍施行於化學工業的各式製程。其中,更以溫室效應所排放的二氧化碳減量回收再利用廣受業界重視。現階段係能以燃燒、熱化學轉換或生物化學轉換等方式,將環境中的二氧化碳加以利用而生成有值甲醇燃料,以期望藉此降低製造甲醇燃料所需耗費的能源,且同時達到環境污染物減量回收再利用之功效。 With the continuous improvement of biomass energy conversion technology, the conversion and utilization of biomass energy has been widely implemented in various processes in the chemical industry. Among them, the reduction and recycling of carbon dioxide emissions from the greenhouse effect has been widely recognized by the industry. At this stage, carbon dioxide in the environment can be utilized to generate valuable methanol fuel by means of combustion, thermochemical conversion or biochemical conversion, in order to reduce the energy required to manufacture methanol fuel and at the same time achieve environmental pollution. The effect of recycling and recycling.

如中華民國公告第I230195號「用生物物質原料製造甲醇之方法及其裝置」專利案,其係使生物物質氣化,再由所產生之生成氣體製造甲醇,該生成氣體係指一氧化碳。其中,係利用日光發電及風力發電等設備所獲得之電力,將水於水電解裝置中電解,並於生成氣體中之氫氣量達到一氧化碳二倍量以上時,令水電解所生成之氫氣供給至前述生成氣體,使其在甲醇合成塔中製造出甲醇。 For example, the Republic of China Announcement No. I230195 "Method and Apparatus for Producing Methanol from Biological Material", which vaporizes biomass, and then produces methanol from the produced gas, which is a carbon monoxide. Among them, the electricity obtained by equipment such as solar power generation and wind power generation is used to electrolyze water in a water electrolysis device, and when the amount of hydrogen in the generated gas reaches twice the amount of carbon monoxide, the hydrogen generated by the water electrolysis is supplied to The gas is generated to produce methanol in a methanol synthesis column.

一般而言,習知製造甲醇之方法,係透過一氧化碳氣 體直接與水電解所產生之氣態氫反應,以合成甲醇燃料。然而,於常溫常壓狀態下,液態水分子中的氫分子與氧分子間鍵結強度,係不容許氫分子與氧分子產生分離,必須自外界通入強電流,使得該液態水分子到達電解能階時,方能使該液態水分子經由電解產出氣態氫分子及氣態氧分子。如此,不僅需消耗大量電能,更須透過長時間電解作用才能釋出足量的氣態氫分子,以致於氣態氫分子的產量明顯受限於電解水分子的反應時間,進而導致氣態氫分子生產效率低落,相對影響後續合成甲醇的效率及產量。 In general, the conventional method for producing methanol is through carbon monoxide gas. The body directly reacts with gaseous hydrogen produced by water electrolysis to synthesize methanol fuel. However, under normal temperature and pressure conditions, the bonding strength between hydrogen molecules and oxygen molecules in liquid water molecules does not allow separation of hydrogen molecules from oxygen molecules, and a strong current must be introduced from the outside to make the liquid water molecules reach electrolysis. When the energy level is enabled, the liquid water molecules can generate gaseous hydrogen molecules and gaseous oxygen molecules via electrolysis. In this way, not only a large amount of electric energy is consumed, but also a sufficient amount of gaseous hydrogen molecules can be released through long-time electrolysis, so that the production of gaseous hydrogen molecules is obviously limited by the reaction time of the electrolyzed water molecules, thereby leading to the production efficiency of gaseous hydrogen molecules. Low, relatively affecting the efficiency and yield of subsequent methanol synthesis.

再且,於電解液態水生成氣態氫分子及氣態氧分子的過程,往往僅將該氣態氫分子用以與一氧化碳作用生成甲醇,而氣態氧分子則無法有效加以利用,著實浪費且不符合能源再利用之目標。 Moreover, in the process of producing gaseous hydrogen molecules and gaseous oxygen molecules in the electrolyte water, the gaseous hydrogen molecules are only used to react with carbon monoxide to form methanol, and the gaseous oxygen molecules cannot be effectively utilized, which is wasteful and does not conform to energy. The goal of utilization.

有鑑於此,確實有必要發展一種提升甲醇生產效率之甲醇製作方法及其裝置,以秉持能源回收再利用之標準,解決如上所述之各種問題。 In view of this, it is indeed necessary to develop a methanol production method and apparatus for improving methanol production efficiency, and to solve the various problems as described above by upholding the standards of energy recovery and reuse.

本發明之主要目的乃改善上述缺點,以提供一種甲醇製作方法,其係能夠以較低耗能自臨界態液態水電解產出氣態氫分子,以有效提升液態水之電解效率者。 The main object of the present invention is to improve the above disadvantages to provide a method for producing methanol which is capable of producing gaseous hydrogen molecules by electrolysis of liquid water from a critical state of lower energy to effectively increase the electrolysis efficiency of liquid water.

本發明之次一目的係提供一種甲醇製作方法,係能夠提高氣態氫分子的產量,以有效提升甲醇生產效率者。 A second object of the present invention is to provide a process for producing methanol which is capable of increasing the production of gaseous hydrogen molecules to effectively increase the efficiency of methanol production.

本發明之再一目的係提供一種甲醇製備裝置,係能夠降低甲醇製作過程所需耗費的能源,以有效達到節省能源 者。 Still another object of the present invention is to provide a methanol preparation apparatus capable of reducing the energy required for a methanol production process to effectively achieve energy saving. By.

本發明之又一目的係提供一種甲醇製備裝置,係能夠將臨界態液態水電解產出的氣態氧分子回收儲存,以符合能源再利用者。 Another object of the present invention is to provide a methanol preparation apparatus capable of recovering and storing gaseous oxygen molecules produced by electrolysis of critical state liquid water to comply with energy reusers.

為達到前述發明目的,本發明之甲醇製作方法,係包含:一前置步驟,係將二氧化碳溶於水,以產生混合有二氧化碳之二相共存水溶液;一轉換步驟,係將該二相共存水溶液進行增壓增溫,使得該二相共存水溶液到達臨界態,而分離出臨界態二氧化碳及臨界水,還原該臨界態二氧化碳而生成臨界態一氧化碳,電解該臨界水而生成超臨界態氫及氧;及一合成步驟,係將該臨界態一氧化碳與該超臨界態氫進行合成反應,以生成甲醇。 In order to achieve the above object, the method for producing methanol of the present invention comprises: a pre-step of dissolving carbon dioxide in water to produce a two-phase coexisting aqueous solution mixed with carbon dioxide; and a converting step of coexisting the two-phase aqueous solution Pressurizing and warming, so that the two-phase coexisting aqueous solution reaches a critical state, and the critical state carbon dioxide and critical water are separated, the critical state carbon dioxide is reduced to generate a critical state of carbon monoxide, and the critical water is electrolyzed to generate supercritical hydrogen and oxygen; And a synthesis step of synthesizing the critical state carbon monoxide with the supercritical hydrogen to form methanol.

其中,該二相共存水溶液所到達之臨界態係指壓力值為221大氣壓,溫度值為672K。再且,該轉換步驟中,係包含有一分離步驟、一還原步驟及一電解步驟,以藉由該分離步驟、還原步驟及電解步驟,獲得臨界態一氧化碳及超臨界態氫。 The critical state reached by the two-phase coexisting aqueous solution means that the pressure value is 221 atmospheres and the temperature value is 672K. Further, in the converting step, a separation step, a reduction step and an electrolysis step are included to obtain a critical state of carbon monoxide and supercritical hydrogen by the separation step, the reduction step and the electrolysis step.

為實施上述甲醇製作方法,本發明更提供一種甲醇製備裝置,其係包含:一混合單元;一轉換單元,係以一管路連通該混合單元,且該轉換單元與混合單元之間係設有至少一加壓件及至少一升溫件,該轉換單元係用以供臨界態氣體產出;及一合成單元,係以另一管路連通該轉換單元,用以供臨界態氣體流入,且該合成單元另連接一排氣管路,用以排出該合成單元內的一合成氣體。 In order to carry out the above methanol production method, the present invention further provides a methanol preparation device, comprising: a mixing unit; a conversion unit connected to the mixing unit by a pipeline, and the conversion unit and the mixing unit are provided At least one pressurizing member and at least one temperature increasing member, wherein the converting unit is used for outputting a critical state gas; and a synthesizing unit is connected to the converting unit by another conduit for supplying a critical state gas, and the The synthesis unit is further connected to an exhaust line for discharging a synthesis gas in the synthesis unit.

其中,該甲醇製備裝置,係能於該電解器以一排氣管 路連通一儲存槽,且於該電解器與儲存槽之間更可以連接有數排熱件,藉此提升節能之效果。 Wherein the methanol preparation device is capable of using an exhaust pipe in the electrolyzer The road is connected to a storage tank, and a plurality of rows of heat members are connected between the electrolyzer and the storage tank, thereby improving the energy saving effect.

為讓本發明之上述及其他目的、特徵及優點能更明顯易懂,下文特舉本發明之較佳實施例,並配合所附圖式,作詳細說明如下:請參照第1圖所示,本發明之甲醇製作方法係包含一前置步驟S1、一轉換步驟S2及一合成步驟S3。 The above and other objects, features, and advantages of the present invention will become more apparent from the aspects of the appended claims. The methanol production method of the present invention comprises a pre-step S1, a conversion step S2 and a synthesis step S3.

該前置步驟S1係選擇將環境中的二氧化碳溶於水,以產生混合有二氧化碳之二相共存水溶液;以將該二相共存水溶液於該轉換步驟S2進行增溫增壓,使得該二相共存水溶液到達臨界態,而分離出臨界態二氧化碳及臨界水,還原該臨界態二氧化碳而生成臨界態一氧化碳,並電解該臨界水而生成超臨界態氫及氧;再於該合成步驟S3中,將該臨界態一氧化碳與該超臨界態氫進行合成反應,而生成甲醇。藉此,係藉由水溶液能快速增溫增壓之特性,使該二相共存水溶液到達臨界態,而以較低耗能自臨界水電解產出氣態氫分子,有效提升液態水之電解效率,達到提升甲醇生成效率及產量之功效。 The pre-step S1 is selected to dissolve the carbon dioxide in the environment into water to generate a two-phase coexisting aqueous solution mixed with carbon dioxide; and to increase the temperature and pressurize the two-phase coexisting aqueous solution in the converting step S2, so that the two phases coexist The aqueous solution reaches a critical state, and the critical state carbon dioxide and the critical water are separated, the critical state carbon dioxide is reduced to generate a critical state carbon monoxide, and the critical water is electrolyzed to generate supercritical hydrogen and oxygen; and in the synthesizing step S3, The critical state carbon monoxide is reacted with the supercritical hydrogen to form methanol. Thereby, the aqueous solution can be rapidly warmed and pressurized, so that the two-phase coexisting aqueous solution reaches a critical state, and the gaseous hydrogen molecules are produced by lower energy consumption from the critical water electrolysis, thereby effectively improving the electrolysis efficiency of the liquid water. Achieve the efficiency of methanol production and production.

本發明僅需透過混合之二相共存水溶液,快速達到臨界態,便能以較低耗能自該臨界水電解產出超臨界態氫及氧,而達成如上所述之功效。本發明為了以較低能耗達到較佳效果,係選擇以多段式增溫增壓方式作為較佳實施例,並詳述於下,熟悉該技藝者係能理解其用意,故不受 限於此實施例。 The invention only needs to pass through the mixed two-phase coexisting aqueous solution to quickly reach the critical state, and the supercritical hydrogen and oxygen can be produced from the critical water electrolysis with lower energy consumption, thereby achieving the above-mentioned effects. In order to achieve better results with lower energy consumption, the present invention selects a multi-stage warming and supercharging method as a preferred embodiment, and is described in detail below. Those skilled in the art can understand the intention, and thus are not Limited to this embodiment.

請再參照第2圖所示,其係為本發明一較佳實施例,該甲醇製作方法係包含一前置步驟S1、一轉換步驟S2及一合成步驟S3。 Referring to FIG. 2 again, which is a preferred embodiment of the present invention, the methanol manufacturing method includes a pre-step S1, a converting step S2, and a synthesizing step S3.

該前置步驟S1係將二氧化碳溶於水,以使混合有二氧化碳之二相共存水溶液轉變為高溫高壓狀態。更詳言之,該二氧化碳係可以來自環境中的含碳空氣污染物,以將空氣中的氣態二氧化碳溶於液態水,而生成混合有二氧化碳的二相共存水溶液。 The pre-step S1 dissolves carbon dioxide in water to convert the two-phase coexisting aqueous solution mixed with carbon dioxide into a high temperature and high pressure state. More specifically, the carbon dioxide system can be derived from carbonaceous air pollutants in the environment to dissolve gaseous carbon dioxide in the air in liquid water to form a two-phase coexisting aqueous solution mixed with carbon dioxide.

較佳者,係於常溫下,對該二相共存水溶液進行加壓,當該二相共存水溶液之壓力值高於1大氣壓後,遂使該二相共存水溶液轉變為高壓態;接著,對高壓態之二相共存水溶液進行加熱,使高壓態之二相共存水溶液逐步加熱至高溫後,該二相共存水溶液係轉變為高溫高壓態(如化學式二所示)。 Preferably, the two-phase coexisting aqueous solution is pressurized at a normal temperature, and when the pressure of the two-phase coexisting aqueous solution is higher than 1 atm, the two-phase coexisting aqueous solution is converted into a high-pressure state; After the two-phase coexisting aqueous solution is heated, the two-phase coexisting aqueous solution is gradually heated to a high temperature, and the two-phase coexisting aqueous solution is converted into a high-temperature and high-pressure state (as shown in Chemical Formula 2).

CO2(aq,T1,P1) → CO2(aq,T2,P2);T1=298K,P1=1atm ;T2=400K,P2=20 atm [化學式二] CO 2 (aq, T1, P1) → CO 2 (aq, T2, P2) ; T1 = 298K, P1 = 1 atm; T2 = 400K, P2 = 20 atm [Chemical Formula 2]

其中,如前所述之「常溫」約指298 K者,係屬熟悉該項技藝者所能理解,於下述內容係以「常溫」作為基準,溫度高於該常溫者,本發明於下所述稱為「高溫」;如前所述之「常壓」約指1大氣壓(atm)者,係屬熟悉該項技藝者所能理解,於下述內容係以「常壓」作為基準,溫度高於該常壓者,本發明於下所述稱為「高壓」。 Among them, the "normal temperature" as mentioned above refers to 298 K, which is familiar to those skilled in the art. The following contents are based on "normal temperature", and the temperature is higher than the normal temperature. The term "atmospheric pressure" as mentioned above; "normal pressure" as mentioned above refers to about 1 atmosphere (atm), which is familiar to those skilled in the art. The following contents are based on "normal pressure". The temperature is higher than the atmospheric pressure, and the present invention is referred to as "high pressure" as described below.

舉例而言,本實施例係將1大氣壓298K的氣態二氧化碳,溶於1大氣壓298K的液態水,以生成1大氣壓298K 之二相共存水溶液;由一泵浦將該1大氣壓298K之二相共存水溶液增壓為20大氣壓330K之二相共存水溶液,再予以進行逐步加熱,以生成400K之二相共存水溶液。 For example, in this embodiment, gaseous carbon dioxide of 298 K at 1 atm is dissolved in liquid water of 298 K at 1 atm to generate 1 atm 298 K. The two-phase coexisting aqueous solution is pressurized by a pump to a two-phase coexisting aqueous solution of 298 K at 1 atm. to a two-phase coexisting aqueous solution of 20 atm and 330 K, and then gradually heated to form a 400 K two-phase coexisting aqueous solution.

該轉換步驟S2係包含一分離步驟S21、一還原步驟S22及一電解步驟S23,透過所述三步驟S21、S22及S23,將該二相共存水溶液增溫增壓至臨界態,而獲得臨界態一氧化碳及超臨界態氫。 The converting step S2 includes a separating step S21, a reducing step S22 and an electrolysis step S23. The three-phase coexisting aqueous solution is heated and pressurized to a critical state through the three steps S21, S22 and S23 to obtain a critical state. Carbon monoxide and supercritical hydrogen.

更詳言之,該分離步驟S2係再次對混合有二氧化態之二相共存水溶液進行加熱,使得該二相共存水溶液到達氣液分離之臨界態,以自該二相共存水溶液中分離出氣態二氧化碳及液態水,且該氣態二氧化碳及液態水均維持於高溫高壓狀態。 More specifically, the separation step S2 is again heating the two-phase coexisting aqueous solution mixed with the two oxidation states, so that the two-phase coexisting aqueous solution reaches a critical state of gas-liquid separation, thereby separating the gaseous state from the two-phase coexisting aqueous solution. Carbon dioxide and liquid water, and the gaseous carbon dioxide and liquid water are maintained at a high temperature and high pressure.

由該分離步驟S21產出高溫高壓氣態二氧化碳後,係於該還原步驟S22中,將高溫高壓氣態二氧化碳通以電流,較佳係選擇通以交流電,且通過一異相觸媒(如含Ni,Ru,Ti之氧化物),以此進行還原反應,生成高溫高壓氣態一氧化碳,更進一步將該高溫高壓氣態一氧化碳進行再增溫增壓,而生成臨界態一氧化碳(如化學式四所示)。 After the high-temperature and high-pressure gaseous carbon dioxide is produced by the separating step S21, the high-temperature and high-pressure gaseous carbon dioxide is passed through the current in the reducing step S22, preferably by alternating current, and passing through a heterogeneous catalyst (eg, containing Ni, Ru). The oxide of Ti is used to carry out a reduction reaction to generate high-temperature and high-pressure gaseous carbon monoxide, and further to increase the temperature of the high-temperature and high-pressure gaseous carbon monoxide to generate a critical state of carbon monoxide (as shown in Chemical Formula 4).

2CO2(g,T2,P2) → 2CO(g,T2,P3)+O2(g,T2,P3);T2=400K,P3=30atm 2CO(g,T2,P3) → 2CO(g,T3,P3);T3=672K,P3=221atm[化學式四] 2CO 2(g, T2, P2) → 2CO (g, T2, P3) + O 2 (g, T2, P3) ; T2 = 400K, P3 = 30atm 2CO (g, T2, P3) → 2CO (g, T3 , P3) ; T3 = 672K, P3 = 221 atm [Chemical Formula 4]

另一方面,該電解步驟S23係將高溫高壓液態水再次以先加壓後升溫之方式,提高該高溫高壓液態水的壓力及溫度值,使得該高溫高壓液態水到達臨界態後,即刻轉變為臨界水。此時,該臨界水分子中的氫鍵鍵結強度明顯低 於一般常溫常壓下之水分子,甚至於低電流的電解作用下,即能快速達到該臨界水分子的電解能階,以便輕易分離該臨界水分子中的氫分子及氧分子,進而生成超臨界態氫及氧(如化學式五所示)。 On the other hand, the electrolysis step S23 is to increase the pressure and temperature of the high-temperature and high-pressure liquid water by first pressurizing and heating the high-temperature and high-pressure liquid water, so that the high-temperature and high-pressure liquid water reaches a critical state and immediately changes to Critical water. At this time, the hydrogen bond strength in the critical water molecule is significantly lower Under the normal temperature and pressure of water molecules, even under the action of low current electrolysis, the critical energy level of the critical water molecules can be quickly reached, so that the hydrogen molecules and oxygen molecules in the critical water molecules can be easily separated, thereby generating super The critical state of hydrogen and oxygen (as shown in Chemical Formula 5).

2H2O(l,T2,P2) → 2H2O(l,T3,P3);T3=672K,P3=221atm 2H2O(l,T3,P3) → 2H2(g,T4,P4)+O2(g,T4,P4);T4=700K,P4=230atm[化學式五] 2H 2 O ( l , T2, P2) → 2H 2 O ( l , T3, P3) ; T3 = 672K, P3 = 221atm 2H 2 O ( l , T3, P3) → 2H 2(g, T4, P4) + O 2 (g, T4, P4) ; T4 = 700K, P4 = 230 atm [Chemical Formula 5]

舉例而言,本實施例係將20大氣壓400K之二相共存水溶液再次升溫,以至該二相共存水溶液之溫度高達672K時且壓力高達221大氣壓,遂能自該二相共存水溶液中電解產出超臨界態二氧化碳與水。其中,該氣態二氧化碳之壓力值係為20大氣壓,且溫度值係為400K;該液態水之壓力值係為20大氣壓,且溫度值係為400K。接著,係通入10~20A之交流電,以此還原該20大氣壓400K之氣態二氧化碳,生成30大氣壓400K之氣態一氧化碳,並以一泵浦將30大氣壓400K之氣態一氧化碳增溫增壓成221大氣壓672K之臨界態一氧化碳,以作為後續合成甲醇之其一原料。 For example, in this embodiment, the two-phase coexisting aqueous solution of 20 atmospheres and 400 K is heated again, so that the temperature of the two-phase coexisting aqueous solution is as high as 672 K and the pressure is as high as 221 atm, and the enthalpy can be electrolyzed from the two-phase coexisting aqueous solution. Critical state carbon dioxide and water. Wherein, the pressure value of the gaseous carbon dioxide is 20 atmospheres, and the temperature value is 400K; the pressure value of the liquid water is 20 atmospheres, and the temperature value is 400K. Then, an alternating current of 10~20A is introduced to reduce the gaseous carbon dioxide of 400K at 20 atmospheres to generate gaseous carbon monoxide of 400K at 30 atmospheres, and the gaseous carbon monoxide of 30 atmospheres of 400 atmosphere is heated and pressurized to 221 atmospheres by 672K with one pump. The critical state of carbon monoxide is used as a raw material for the subsequent synthesis of methanol.

另一方面,係由一泵浦將20大氣壓400K之液態水壓縮為221大氣壓之液態水,並且繼續以逐步加熱之方式,使液態水升溫至672K而轉變為臨界水,再通入電流進行電解反應,以到達該臨界水的電解能階後,即可自該臨界水分離出超臨界態氫及氧,且該氫及氧係維持於壓力為230大氣壓,及溫度為700K之超臨界狀態。其中,該超臨界態氫係用以作為後續合成甲醇的另一原料,而該超臨界 氧係能加以回收儲存,以作為其他工業製程所需之用。 On the other hand, a pump is used to compress liquid water of 20 atmospheres and 400K into liquid water of 221 atmospheres, and continue to heat the liquid water to 672K in a stepwise heating manner to be converted into critical water, and then conduct current for electrolysis. After the reaction reaches the electrolysis energy level of the critical water, the supercritical hydrogen and oxygen can be separated from the critical water, and the hydrogen and oxygen are maintained at a pressure of 230 atm and a supercritical state at a temperature of 700K. Wherein the supercritical hydrogen is used as another raw material for the subsequent synthesis of methanol, and the supercritical Oxygen can be recovered and stored for use in other industrial processes.

該合成步驟S3係將該臨界態一氧化碳與該超臨界態氫進行合成反應,以生成氣態甲醇(如化學式六所示)。更詳言之,本實施例係以221大氣壓672K之超臨界態一氧化碳,與該230大氣壓700K之超臨界氣態氫進行反應,以於充分合成作用下,生成氣態甲醇。 The synthesizing step S3 synthesizes the critical state carbon monoxide with the supercritical hydrogen to form gaseous methanol (as shown in Chemical Formula 6). More specifically, this example is a supercritical gaseous carbon of 221 atmospheres of 672 K and reacted with a supercritical gaseous hydrogen of 230 atmospheres at 700 atmospheres to form gaseous methanol under sufficient synthesis.

CO(g,T3,P3)+2H2(g,T4,P4) → CH3OH(g,T5,P5);T5=730K,P5=77 atm[化學式六] CO (g, T3, P3) + 2H 2 (g, T4, P4) → CH 3 OH (g, T5, P5) ; T5 = 730K, P5 = 77 atm [Chemical Formula 6]

如上述,本發明之甲醇製作方法,係能於二氧化碳氣體溶於液態水後,透過液態分子間距離較氣態分子間距離緊密之特性,輕易予以加壓升溫,並於後續透過階段性的氣液分離,使該氣態二氧化碳能夠於交流電流作用下,還原生成氣態一氧化碳,並且將該氣態一氧化碳再增溫增壓為臨界態一氧化碳;同時,更可以經由再次加壓升溫之過程,使液態水快速轉變為臨界水,以降低水分子中的氫鍵鍵結強度,而輕易於電解作用下達到氫分子及氧分子的解離能階,快速自該臨界水中分離出超臨界態氫及氧,藉此提升超臨界態氫的生成效率,以由該臨界態一氧化碳與超臨界態氫合成甲醇。如此,本發明之甲醇製作方法,係能利用臨界態達到提升液態水電解生成超臨界態氫之效率,且同時於短時間內增加該超臨界態氫的產出量,而能透過大量超臨界態氫與該臨界態一氧化碳反應,以相對達到提升甲醇生成效率及產量之功效。 As described above, the method for producing methanol according to the present invention is capable of easily pressurizing and heating the carbon dioxide gas after being dissolved in liquid water, and the distance between the liquid molecules is tighter than the distance between the gaseous molecules, and then passing through the staged gas and liquid. Separating, the gaseous carbon dioxide can be reduced to form gaseous carbon monoxide under the action of alternating current, and the gaseous carbon monoxide is further heated and pressurized to a critical state of carbon monoxide; at the same time, the liquid water can be rapidly transformed through the process of repressurizing and heating up. It is a critical water to reduce the hydrogen bonding strength in water molecules, and it is easy to achieve the dissociation energy level of hydrogen molecules and oxygen molecules under electrolysis, and rapidly remove supercritical hydrogen and oxygen from the critical water, thereby improving The formation efficiency of supercritical hydrogen is to synthesize methanol from the critical state of carbon monoxide and supercritical hydrogen. Thus, the methanol production method of the present invention can utilize the critical state to increase the efficiency of liquid water electrolysis to generate supercritical hydrogen, and at the same time increase the output of the supercritical hydrogen in a short time, and can pass a large amount of supercritical The hydrogen reacts with the critical state of carbon monoxide to relatively improve the efficiency of methanol production and the yield.

請參照第3圖所示,其係為一用以製備甲醇之裝置,該甲醇製備裝置係為本發明的一較佳實施例,以作為進一 步詳述本發明甲醇製作方法之用。 Please refer to FIG. 3, which is a device for preparing methanol. The methanol preparation device is a preferred embodiment of the present invention, as a further The steps are used to describe the methanol production process of the present invention.

該甲醇製備裝置係包含一混合單元1、一轉換單元2及一合成單元3。於各該單元之間係分別以不同之管路連通,以構成該甲醇製備裝置之連續通路,詳述如下。 The methanol preparation device comprises a mixing unit 1, a conversion unit 2 and a synthesis unit 3. Each of the units is connected by a different conduit to form a continuous passage of the methanol preparation unit, as described in detail below.

該混合單元1係用以供反應物料進行混合,以確保該反應物料能以液體狀態流入後續管路。本實施例較佳係選擇以冷卻吸收塔作為混合單元1,藉此確保進入該混合單元1內的二氧化碳,能完全溶於液態水,以節省後續加壓加溫時所需耗費的能量。 The mixing unit 1 is used to mix the reaction materials to ensure that the reaction materials can flow into the subsequent pipelines in a liquid state. In this embodiment, the cooling absorption tower is preferably selected as the mixing unit 1, thereby ensuring that the carbon dioxide entering the mixing unit 1 is completely dissolved in the liquid water to save the energy required for the subsequent pressurization heating.

該轉換單元2係以一管路T1連通該混合單元1,且該轉換單元2與混合單元1之間係設有至少一加壓件P及至少一升溫件H,該轉換單元2係用以供臨界氣體產出。該加壓件P係用以壓縮自該混合單元1流經該管路T1之二相共存水溶液,該升溫件H係透過該管路T1連接該加壓件P,以加熱自該混合單元流經該管路T1之二相共存水溶液,使得該二向共存水溶液轉為高溫高壓狀態,甚至幾近臨界態而進入該轉換單元2。 The conversion unit 2 is connected to the mixing unit 1 by a pipe T1, and at least one pressing member P and at least one temperature increasing member H are disposed between the converting unit 2 and the mixing unit 1. The conversion unit 2 is used for For critical gas production. The pressurizing member P is for compressing the two-phase coexisting aqueous solution flowing through the pipe T1 from the mixing unit 1, and the temperature increasing member H is connected to the pressurizing member P through the pipe T1 to heat the flow from the mixing unit. The two-phase coexisting aqueous solution passes through the two-phase coexisting aqueous solution of the line T1, so that the two-way coexisting aqueous solution is turned into a high temperature and high pressure state, and even into a near critical state, enters the conversion unit 2.

該轉換單元2係包含一分離器21、一還原器22及一電解器23,該分離器21係透過該管路T1連通該混合單元1,用以承裝流經該管路T1之二相共存水溶液,而分離輸出氣態二氧化碳及液態水;且該分離器21係以一第一分支管路T21連通該還原器22,用以供自該分離器21產生之氣態二氧化碳流通;該電解器23與該分離器21之間設有相互連通的一第二分支管路T22,以將流通於該第二分支管路T22之液態水導入該電解器23,由該電解器23解離 出該臨界水中的氫分子及氧分子,以便將該超臨界態氫及氧各別排出,其中,該二相共存水溶液係由二氧化碳溶於水所生成,且該加壓件P較佳係選擇為一泵浦。 The conversion unit 2 comprises a separator 21, a reducer 22 and an electrolyzer 23, and the separator 21 communicates with the mixing unit 1 through the pipeline T1 for receiving two phases flowing through the pipeline T1. The aqueous solution is coexisted to separate and output gaseous carbon dioxide and liquid water; and the separator 21 is connected to the reducer 22 by a first branch line T21 for supplying gaseous carbon dioxide generated from the separator 21; the electrolyzer 23 A second branch line T22 communicating with each other is disposed between the separator 21 to introduce liquid water flowing through the second branch line T22 into the electrolyzer 23, and is dissociated by the electrolyzer 23. Hydrogen molecules and oxygen molecules in the critical water are discharged to separate the supercritical hydrogen and oxygen, wherein the two-phase coexisting aqueous solution is formed by dissolving carbon dioxide in water, and the pressurizing member P is preferably selected. For a pump.

該合成單元3係以另一管路連通該轉換單元2,用以供臨界態氣體流入,且該合成單元3另連接一排氣管路T30,用以排出該合成單元3內的一合成氣體。更詳言之,本實施例之合成單元3係以二進氣管路T31、T32各別連通該還原器22及電解器23,該進氣管路T31係用以供自該還原器22產出之氣態一氧化碳流通,該進氣管路T32係用以供自該電解器23產出之超臨界態氫流通,且該二進氣管路T31、T32係同時匯流於該合成單元3,以於該合成單元3進行臨界態一氧化碳與超臨界態氫之合成,藉此產出甲醇氣體,並由該排氣管路T30排出該甲醇氣體。 The synthesis unit 3 is connected to the conversion unit 2 by another pipeline for supplying a critical state gas, and the synthesis unit 3 is further connected to an exhaust line T30 for discharging a synthesis gas in the synthesis unit 3. . More specifically, the synthesizing unit 3 of the present embodiment connects the reducer 22 and the electrolyzer 23 to each of the two intake lines T31 and T32, and the intake line T31 is used for the production of the reducer 22 The gaseous carbon monoxide flows out, the intake line T32 is used for the supercritical hydrogen flow from the electrolyzer 23, and the two intake lines T31 and T32 are simultaneously merged with the synthesizing unit 3 to The synthesis unit 3 performs synthesis of a critical state of carbon monoxide and supercritical hydrogen, thereby producing methanol gas, and the methanol gas is discharged from the exhaust line T30.

為了因應本發明較佳實施例之多段式增溫增壓方式,請參照第4圖所示,本實施例之第二分支管路T22及進氣管路T31係個別連接一加壓件P1及一升溫件H1。 In order to respond to the multi-stage warming and supercharging method of the preferred embodiment of the present invention, please refer to FIG. 4, the second branch line T22 and the intake line T31 of the embodiment are individually connected with a pressurizing member P1 and A heating element H1.

如此,該管路T1所連接之加壓件P及升溫件H,僅需使自該混合單元1流經該管路T1之常溫常壓二相共存水溶液,轉變為高溫高壓狀態,以便使該二相共存水溶液攜帶高熱能進入該分離器21即可。此時,該分離器21係用以承裝高溫高壓的二相共存水溶液,且該分離器21另設有一輔助加熱件211,該輔助加熱件211則進一步供給高溫高壓二相共存水溶液更高熱能,以確保該高溫高壓的二相共存水溶液,能於該分離器21達到氣液分離之溫度,藉此自該分離器21輸出氣態二氧化碳及液態水。其中,該分 離器21的細部結構設計及氣液分離原理,係屬熟悉該項技藝者所能理解,故於此不再詳加贅述。 In this way, the pressurizing member P and the temperature increasing member H to which the pipe T1 is connected need only change the normal temperature and normal pressure two-phase coexisting aqueous solution flowing through the pipe T1 from the mixing unit 1 to a high temperature and high pressure state, so that the The two-phase coexisting aqueous solution can carry high heat energy into the separator 21. At this time, the separator 21 is used for supporting a high-temperature and high-pressure two-phase coexisting aqueous solution, and the separator 21 is further provided with an auxiliary heating member 211, and the auxiliary heating member 211 further supplies a high-temperature and high-pressure two-phase coexisting aqueous solution with higher heat energy. In order to ensure the high temperature and high pressure two-phase coexisting aqueous solution, the separator 21 can reach the temperature of the gas-liquid separation, thereby outputting gaseous carbon dioxide and liquid water from the separator 21. Among them, the score The detailed structural design of the separator 21 and the principle of gas-liquid separation are understood by those skilled in the art, and thus will not be described in detail herein.

再且,本實施例較佳係透過該分離器21上方的一氣體收集器(未繪示),吸附產自該分離器21之氣態二氧化碳後,由該第一分支管路T21將該氣態二氧化碳導入該還原器22,且該還原器22另連接有一電流供應件221,該電流供應件221較佳係用以供給該還原器22足夠之交流電,以便將該還原器22內之氣態二氧化碳進行還原,而生成氣態一氧化碳。 Moreover, the present embodiment preferably transmits a gaseous carbon dioxide from the first branch line T21 after passing through a gas collector (not shown) above the separator 21 to adsorb gaseous carbon dioxide produced from the separator 21. The reducer 22 is further connected to a current supply member 221, and the current supply member 221 is preferably used to supply the reducer 22 with sufficient alternating current to restore the gaseous carbon dioxide in the reducer 22. And generate gaseous carbon monoxide.

另外,本實施例之電解器23係以該第二分支管路T22連通該分離器21,且該電解器23所連接之加壓件P1係用以壓縮自該分離器21流經該第二分支管路T22之液態水,以便使該液態水到達臨界壓力值,且該加壓件P1較佳係選擇為一泵浦,該泵浦僅用以提高液態水之壓力,而使液態水維持原有之溫度;該電解器23所連接之升溫件H1係用以加熱該液態水到達臨界溫度值,以便使該液態水轉變為臨界水而流入該電解器23。此時,該電解器23係以另一電流供應件231供給適當之電流,以達到該臨界水的電解能階後,藉此由該電解器23解離出該臨界水中的氫分子及氧分子,以便將該超臨界態氫及氧各別排出。其中,該電解器23的細部結構設計及電解原理,係屬熟悉該項技藝者所能理解,故於此不再詳加贅述。 In addition, the electrolyzer 23 of the present embodiment is connected to the separator 21 by the second branch line T22, and the pressurizing member P1 connected to the electrolyzer 23 is used for compressing from the separator 21 through the second. The liquid water of the branch line T22 is branched so that the liquid water reaches a critical pressure value, and the pressurizing member P1 is preferably selected as a pump, and the pump is only used to increase the pressure of the liquid water, and the liquid water is maintained. The original temperature; the temperature riser H1 connected to the electrolyzer 23 is used to heat the liquid water to a critical temperature value, so that the liquid water is converted into critical water and flows into the electrolyzer 23. At this time, the electrolyzer 23 supplies an appropriate current to the other current supply member 231 to reach the electrolysis energy level of the critical water, whereby the electrolyzer 23 dissociates the hydrogen molecules and the oxygen molecules in the critical water. In order to discharge the supercritical hydrogen and oxygen separately. The detailed structural design and electrolysis principle of the electrolyzer 23 are understood by those skilled in the art, and thus will not be described in detail herein.

於本實施例中,該合成單元3係能藉由該進氣管路T31之加壓件P2及升溫件H2,將流通於該進器管路T31之氣態一氧化碳轉變為臨界態一氧化碳,以於該合成單元 3內與超臨界態氫進行合成反應,藉此產出甲醇氣體,並由該排氣管路T30排出該甲醇氣體,作為工業製程之燃料能源。 In the present embodiment, the synthesizing unit 3 can convert the gaseous carbon monoxide flowing through the feeder line T31 into a critical state of carbon monoxide by the pressurizing member P2 and the temperature increasing member H2 of the intake line T31. The synthesis unit 3 is internally reacted with supercritical hydrogen to thereby produce methanol gas, and the methanol gas is discharged from the exhaust line T30 as a fuel source for an industrial process.

此外,該電解器23還可以以一輸氣管路T23連通一儲存槽4,藉此透過該輸氣管路T23輸送自該電解器23產出之超臨界態氧,使得該超臨界態氧能儲存於該儲存槽4,以供其他工業製程所需之用。且,於該電解器23與儲存槽4之間更可以連接有數排熱件(未繪示),以藉由該排熱件達到節能之功效。 In addition, the electrolyzer 23 can also be connected to a storage tank 4 by a gas pipeline T23, whereby the supercritical oxygen produced from the electrolyzer 23 is sent through the gas pipeline T23, so that the supercritical oxygen can be stored. In the storage tank 4, it is used for other industrial processes. Moreover, a plurality of heat-dissipating members (not shown) may be connected between the electrolyzer 23 and the storage tank 4 to achieve energy-saving effect by the heat-dissipating member.

於此,本發明甲醇製備裝置,係能以簡易的設備連通設計,操作本發明甲醇製作之方法,以達到如上所述提升液態水電解生成超臨界態氫之效率,且同時於短時間內增加該超臨界態氫的產出量,而能透過超臨界態氫大量與該臨界態一氧化碳反應,以相對達到提升甲醇生成效率及產量之功效。甚至,本發明甲醇製備裝置更可以降低製程能源的耗損,且將不需反應之液態氧加以回收儲存,進一步達成節省能源及能源再利用之功效。 Herein, the methanol preparation device of the present invention can operate the methanol production method of the present invention in a simple device communication design to achieve the efficiency of evaporating liquid water to generate supercritical hydrogen as described above, and simultaneously increase in a short time. The output of the supercritical hydrogen is capable of reacting with the critical state of carbon monoxide through a large amount of supercritical hydrogen to relatively improve the efficiency of methanol production and the yield. In addition, the methanol preparation device of the invention can reduce the consumption of process energy, and recover and store the liquid oxygen that does not need to be reacted, thereby further achieving the effects of energy conservation and energy reuse.

本發明之甲醇製作方法,係能夠以較低耗能自臨界態液態水電解產出氣態氫分子,以達到有效提升液態水電解效率之功效。 The method for preparing methanol of the invention is capable of producing gaseous hydrogen molecules by electrolysis of liquid water with a lower energy consumption from a critical state, so as to effectively improve the electrolysis efficiency of liquid water.

本發明甲醇製作方法,係能夠提高氣態氫分子的產量,以達到有效提升甲醇生產效率之功效。 The method for preparing methanol of the invention can improve the yield of gaseous hydrogen molecules, so as to effectively improve the efficiency of methanol production.

本發明之甲醇製備裝置,係能夠降低甲醇製作過程所需耗費的能源,以達到有效節省能源之功效。 The methanol preparation device of the invention can reduce the energy required for the methanol production process, thereby achieving the effect of effectively saving energy.

本發明之甲醇製備裝置,係能夠將臨界態液態水電解 產出的氣態氧分子回收儲存,以達到能源再利用之功效。 The methanol preparation device of the invention is capable of electrolyzing a critical state liquid water The produced gaseous oxygen molecules are recovered and stored to achieve the effect of energy reuse.

雖然本發明已利用上述較佳實施例揭示,然其並非用以限定本發明,任何熟習此技藝者在不脫離本發明之精神和範圍之內,相對上述實施例進行各種更動與修改仍屬本發明所保護之技術範疇,因此本發明之保護範圍當視後附之申請專利範圍所界定者為準。 While the invention has been described in connection with the preferred embodiments described above, it is not intended to limit the scope of the invention. The technical scope of the invention is protected, and therefore the scope of the invention is defined by the scope of the appended claims.

〔本發明〕 〔this invention〕

S1‧‧‧前置步驟 S1‧‧‧Pre-steps

S2‧‧‧轉換步驟 S2‧‧‧ conversion steps

S21‧‧‧分離步驟 S21‧‧‧Separation step

S22‧‧‧還原步驟 S22‧‧‧Reduction steps

S23‧‧‧電解步驟 S23‧‧‧ Electrolysis step

S3‧‧‧合成步驟 S3‧‧‧Synthesis step

1‧‧‧混合單元 1‧‧‧Mixed unit

2‧‧‧轉換單元 2‧‧‧Conversion unit

21‧‧‧分離器 21‧‧‧Separator

211‧‧‧輔助加熱件 211‧‧‧Auxiliary heating parts

22‧‧‧還原器 22‧‧‧Restore

221‧‧‧電流供應件 221‧‧‧current supply parts

23‧‧‧電解器 23‧‧‧ Electrolyzer

231‧‧‧電流供應件 231‧‧‧ Current supply parts

3‧‧‧合成單元 3‧‧‧Synthesis unit

4‧‧‧儲存槽 4‧‧‧ storage tank

T1‧‧‧管路 T1‧‧‧ pipeline

T21‧‧‧第一分支管路 T21‧‧‧First branch line

T22‧‧‧第二分支管路 T22‧‧‧Second branch pipeline

T23‧‧‧輸氣管路 T23‧‧‧ gas pipeline

T30‧‧‧排氣管路 T30‧‧‧ exhaust line

T31‧‧‧進氣管路 T31‧‧‧ intake line

T32‧‧‧進氣管路 T32‧‧‧ intake line

P、P1、P2‧‧‧加壓件 P, P1, P2‧‧‧ pressure parts

H、H1、H2‧‧‧升溫件 H, H1, H2‧‧‧ heating parts

第1圖:本發明甲醇製作方法之流程示意圖。 Fig. 1 is a schematic view showing the flow of a process for producing methanol according to the present invention.

第2圖:本發明甲醇製作方法之又一流程示意圖。 Fig. 2 is a schematic view showing still another flow of the methanol production method of the present invention.

第3圖:本發明甲醇製備裝置之裝置示意圖。 Figure 3 is a schematic view of the apparatus of the methanol preparation apparatus of the present invention.

第4圖:本發明甲醇製備裝置之又一裝置示意圖。 Figure 4 is a schematic view of still another apparatus of the methanol preparation apparatus of the present invention.

S1‧‧‧前置步驟 S1‧‧‧Pre-steps

S2‧‧‧轉換步驟 S2‧‧‧ conversion steps

S3‧‧‧合成步驟 S3‧‧‧Synthesis step

Claims (19)

一種甲醇製作方法,係包含:一前置步驟,係將二氧化碳溶於水,以產生混合有二氧化碳之二相共存水溶液;一轉換步驟,係將該二相共存水溶液進行增壓增溫,分離出氣態二氧化碳及液態水,再分別增壓增溫,以獲得臨界態二氧化碳及臨界水,還原該臨界態二氧化碳而生成臨界態一氧化碳,電解該臨界水而生成超臨界態氫及氧;及一合成步驟,係將該臨界態一氧化碳與該超臨界態氫進行合成反應,以生成甲醇。 A method for preparing methanol comprises: a pre-step of dissolving carbon dioxide in water to produce a two-phase coexisting aqueous solution mixed with carbon dioxide; and a converting step of pressurizing and heating the two-phase coexisting aqueous solution to separate and separate Gaseous carbon dioxide and liquid water are separately pressurized and warmed to obtain critical state carbon dioxide and critical water, reduce the critical state carbon dioxide to form critical state carbon monoxide, electrolyze the critical water to generate supercritical hydrogen and oxygen; and a synthesis step And synthesizing the critical state carbon monoxide with the supercritical hydrogen to form methanol. 依申請專利範圍第1項所述之甲醇製作方法,該臨界態二氧化碳及臨界水所到達之臨界態係指壓力值為221大氣壓,溫度值為672K。 According to the methanol production method described in the first paragraph of the patent application, the critical state reached by the critical state carbon dioxide and the critical water means that the pressure value is 221 atmospheres and the temperature value is 672K. 依申請專利範圍第1或2項所述之甲醇製作方法,於該前置步驟中,係先將該二相共存水溶液進行增溫增壓,以使混合有二氧化碳之二相共存水溶液轉變為高溫高壓狀態。 According to the method for preparing methanol according to claim 1 or 2, in the pre-step, the two-phase coexisting aqueous solution is first heated and pressurized to convert the two-phase coexisting aqueous solution mixed with carbon dioxide into a high temperature. High pressure state. 依申請專利範圍第3項所述之甲醇製作方法,於該前置步驟中的高溫高壓狀態係指壓力為20大氣壓,且溫度為330K以上。 According to the methanol production method described in the third paragraph of the patent application, the high temperature and high pressure state in the pre-step means that the pressure is 20 atm and the temperature is 330 K or more. 依申請專利範圍第3項所述之甲醇製作方法,於該轉換步驟中,係包含有一分離步驟、一還原步驟及一電解步驟,以藉由該分離步驟、還原步驟及電解步驟,獲得臨 界態一氧化碳及超臨界態氫。 According to the method for preparing methanol according to claim 3, in the converting step, a separation step, a reduction step and an electrolysis step are included to obtain the separation step, the reduction step and the electrolysis step. Boundary carbon monoxide and supercritical hydrogen. 依申請專利範圍第5項所述之甲醇製作方法,該分離步驟係先自該二相共存水溶液中分離出高溫高壓的氣態二氧化碳及高溫高壓液態水。 According to the method for preparing methanol according to claim 5, the separation step first separates high-temperature and high-pressure gaseous carbon dioxide and high-temperature high-pressure liquid water from the two-phase coexisting aqueous solution. 依申請專利範圍第5項所述之甲醇製作方法,該還原步驟係將該高溫高壓氣態二氧化碳還原為高溫高壓氣態一氧化碳,再將該高溫高壓氣態一氧化碳增溫增壓為臨界態一氧化碳。 According to the methanol production method described in claim 5, the reduction step is to reduce the high-temperature and high-pressure gaseous carbon dioxide to high-temperature and high-pressure gaseous carbon monoxide, and then pressurize the high-temperature and high-pressure gaseous carbon monoxide to a critical state of carbon monoxide. 依申請專利範圍第7項所述之甲醇製作方法,於該還原步驟中,係通入10至20A之電流,以使高溫高壓氣態二氧化碳生成高溫高壓氣態一氧化碳,並將壓力值30大氣壓,溫度值為400K之氣態一氧化碳,壓縮為壓力值221大氣壓,溫度值係為672K之臨界態一氧化碳。 According to the methanol production method described in claim 7 of the patent application, in the reduction step, a current of 10 to 20 A is introduced to generate high temperature and high pressure gaseous carbon dioxide to generate high temperature and high pressure gaseous carbon monoxide, and the pressure value is 30 atmospheres, and the temperature value is It is 400K gaseous carbon monoxide, compressed to a pressure of 221 atmospheres, and the temperature value is 672K of critical state carbon monoxide. 依申請專利範圍第5項所述之甲醇製作方法,該電解步驟係將該高溫高壓液態水進行再增溫增壓,使得該高溫高壓液態水到達臨界態,而生成臨界水,以將該臨界水電解生成超臨界態氫及氧。 According to the method for preparing methanol according to claim 5, the electrolysis step is to re-temperature and pressurize the high-temperature and high-pressure liquid water, so that the high-temperature and high-pressure liquid water reaches a critical state, and a critical water is generated to the critical point. Water electrolysis produces supercritical hydrogen and oxygen. 依申請專利範圍第9項所述之甲醇製作方法,於該電解步驟中,該高溫高壓液態水所到達之臨界態係指壓力值為221大氣壓,溫度值為672K,且該超臨界態氫及氧的壓力值為230大氣壓,溫度值為700K。 According to the method for preparing methanol according to claim 9 of the patent application, in the electrolysis step, the critical state reached by the high-temperature and high-pressure liquid water means a pressure value of 221 atm, a temperature value of 672 K, and the supercritical hydrogen and The oxygen pressure value is 230 atmospheres and the temperature value is 700K. 一種甲醇製備裝置,係包含:一混合單元;一轉換單元,係以一管路連通該混合單元,且該轉換單元與混合單元之間係設有至少一加壓件及至少一升溫 件,該轉換單元係用以供臨界態氣體產出;及一合成單元,係以另一管路連通該轉換單元,用以供臨界態氣體流入,且該合成單元另連接一排氣管路,用以排出該合成單元內的一合成氣體。 A methanol preparation device comprises: a mixing unit; a conversion unit connected to the mixing unit by a pipeline, and at least one pressing member and at least one temperature rising between the conversion unit and the mixing unit The conversion unit is for outputting a critical state gas; and a synthesis unit is connected to the conversion unit by another pipeline for supplying a critical state gas, and the synthesis unit is further connected to an exhaust line For discharging a synthesis gas in the synthesis unit. 依申請專利範圍第11項所述之甲醇製備裝置,其中該轉換單元係包含有一分離器、一還原器及一電解器,該分離器係以一第一分支管路連通該還原器,且該分離器與該電解器之間設有相互連通的一第二分支管路。 The methanol preparation device according to claim 11, wherein the conversion unit comprises a separator, a reducer and an electrolyzer, the separator is connected to the reducer by a first branch line, and the A second branch line communicating with each other is disposed between the separator and the electrolyser. 依申請專利範圍第12項所述之甲醇製備裝置,其中該合成單元係以二進氣管路各別連通該還原器及電解器。 The methanol preparation device according to claim 12, wherein the synthesis unit is connected to the reducer and the electrolyzer by two intake lines. 依申請專利範圍第13項所述之甲醇製備裝置,其中該第一分支管路與連接該還原器之進氣管路係個別連接一加壓件及一升溫件。 The methanol preparation device according to claim 13, wherein the first branch line and the inlet line connecting the reducer are individually connected with a pressing member and a temperature rising member. 依申請專利範圍第12項所述之甲醇製備裝置,其中該還原器連接有一電流供應件,該電流供應件係用以供給電流於該還原器。 The methanol preparation device according to claim 12, wherein the reducer is connected to a current supply member for supplying current to the reducer. 依申請專利範圍第12項所述之甲醇製備裝置,其中該電解器另連接有另一電流供應件,該電流供應件係用以供給電流於該電解器。 The methanol preparation device according to claim 12, wherein the electrolyzer is further connected with another current supply member for supplying current to the electrolyzer. 依申請專利範圍第12項所述之甲醇製備裝置,其中該電解器另以一排氣管路連通一儲存槽。 The methanol preparation device according to claim 12, wherein the electrolyzer is connected to a storage tank by an exhaust line. 依申請專利範圍第17項所述之甲醇製備裝置,於該電解器與該儲存槽之間另連接有數排熱件。 According to the methanol preparation device described in claim 17, a plurality of rows of heat members are further connected between the electrolyzer and the storage tank. 依申請專利範圍第12項所述之甲醇製備裝置,其中該分離器另設有一輔助加熱件,該輔助加熱件係用以對該 分離器進行升溫。 The methanol preparation device according to claim 12, wherein the separator is further provided with an auxiliary heating member for The separator is heated.
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